CN101530713B - Recovering and purifying device of organic solvent and method - Google Patents
Recovering and purifying device of organic solvent and method Download PDFInfo
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- CN101530713B CN101530713B CN2009100476411A CN200910047641A CN101530713B CN 101530713 B CN101530713 B CN 101530713B CN 2009100476411 A CN2009100476411 A CN 2009100476411A CN 200910047641 A CN200910047641 A CN 200910047641A CN 101530713 B CN101530713 B CN 101530713B
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Abstract
The invention provides a recovering and purifying device of an organic solvent and a method. The invention is characterized in that a first absorber and a second absorber which operate alternatively are adopted to purify waste gas and are desorbed by adopting gas with low oxygen content. The desorption of adsorbents by adopting a closed loop system with low oxygen content has the following benefits: the closed loop effectively improves partial pressure of organic gas under the condition of not having influence on heat transmission rate and is beneficial to condensation and separation; due to the closed loop, the total oxygen content of gas in the loop is controlled so as to lead the probability that organic matters in the regenerative process have chemical change to be reduced greatly; the quality of the recovered organic matters is better; and low oxygen content ensures the safety of the system. Under the premise of guaranteeing the recovering yield, the device and the method effectively improve efficiency of energy utilization in the desorption process, simultaneously the obtained organic matters have high purity, the subsequent refining cost is low, and the application range of absorption separation and absorption recovery of gaseous pollutants is expanded.
Description
Technical field
The present invention relates to a kind of organic solvent reclaiming clean device and method, belong to the environment-friendly and energy-saving emission-reduction technical field.
Background technology
Solvent is meant and can dissolves the inorganic of other gaseous states, liquid state or solid matter or organic liquid material.In industrial production, using more is organic solvent.(Volatile Organic Compounds is called for short VOCs and organic solvent all belongs to volatile organic matter.Saturated vapour pressure was greater than the organic matter of 71Pa when VOCs typically referred under normal pressure boiling point and is lower than 260 ℃ or room temperature, and saturated vapour pressure is called VOCs greater than the organic matter of 13Pa when also having the scholar that boiling point under the normal pressure is lower than 100 or 25 ℃.
Dimethylbenzene is mainly derived from the volatilization that is coated with the part surface in the baking room gas, its concentration and the turnover rate of waiting to dry part, and baking room temperature and ventilation rate etc. are relevant.Also contain a certain amount of particle (concrete amount depends on particle content in the baking room surrounding air) in the gas, different with the spraying workshop section exhaust of upstream, the content of coating cloud is very little in the gas.Gas temperature is basic identical with the baking room temperature.
Technically, the purification process technique of gaseous organic pollutant comprises separation and transforms purification two broad aspect.Methods such as the burning in the gaseous organic pollutant treatment process, catalyzed conversion and biological cleaning all belong to pure conversion purification process, can not reclaim useful organic matter.The purification of gaseous organic substance is reclaimed can adopt methods such as film separation, absorption, absorption, condensation.Film separates and need carry out under the operation with high pressure condition, and the gas film parting material also is in continuous development stages, only is suitable for the occasion of little air quantity, high concentration usually.Absorption process mainly adopts other liquid organic solvent that gas is carried out absorption cleaning, separates by modes such as rectifying again, and the selection of absorbent and the post processing of absorption liquid make it be fit to use some specific occasions.Condensation method reclaims the Purasiv HR of the organic final U.S. of gas union carhide company and the Polyad fluid bed adsorption system of AIIIerican punfication company often.To handle load big although mobile fluid bed has, and the mass-and heat-transfer condition is good, mobile fluid bed to the flowability of adsorbent, come source problem and hardness higher, the equipment of adding is very complicated, so practical application is considerably less.
Adsorption cleaning has obtained using widely in a lot of industries as the unit operations technology of classics.Adsorption process is an enrichment method technology in essence.It is one of core of whole process that desorption in the adsorption process reclaims.Traditional desorption method has water vapour, hot gas desorption, the transformation desorption, and new desorption methods such as electrothermal way, oxidation reclaiming process, ultrasonic regeneration method have appearred again in solvent exchange in recent years.For the desorption that is adsorbed with lower low-molecular-weight hydrocarbon of boiling point and the organic saturated charcoal of aromatic series, better suited is water vapour, hot gas desorption method.The water vapour heat content is high and be easy to get, and desorption economy and security are better, but for the material desorption ability of higher a little less than, need the long desorption cycle, easily cause the corrosion of system, to the raising of system material performance requirement; Water content is higher in the material that reclaims, the secondary pollution problem that also has condensed water, desorb can influence the quality of regenerant when being easy to the pollutant (as halogenated hydrocarbons) of hydrolysis, the adsorption system behind the steam desorption needs the cool drying of long period, could come into operation once more.Compare with the steam desorb, the condensed water secondary pollution of hot gas desorb seldom, the organic matter water content of recovery low (for the more apparent advantage of water miscible organic matter) is convenient to further refining the recovery, the time of regeneration of adsorbent beds drying, cooling is shorter, and is relatively low to the adsorption system material requirements.The shortcoming of hot gas desorption is directly to adopt the hot-air desorb, may have certain danger, and the existence of oxygen can influence the quality of recover materials.
Summary of the invention
The purpose of this invention is to provide a kind of safe, energy consumption is low, the inert gas consumption is low, the recovery time is short, the organic solvent reclaiming clean device and method of recover materials quality better.
In order to achieve the above object, technical scheme of the present invention provides a kind of organic solvent recovery and purification method, it is characterized in that, concrete steps are:
The waste gas that will contain organic solvent is pre-chilled to 40-100 ℃, is cooled to 10-40 ℃ again, and waste gas cooled is fed at least one absorber, will export after 100-200 ℃ through the heating by the exhaust gases of adsorption treatment;
Wherein, the desorption of described absorber is: the low oxygen content gas feeding absorber that will be preheating to 150-300 ℃ carries out desorption; When the temperature of absorber surpasses 90 ℃ and desorption time and reaches 15-30min, after constantly 1/100-1/2 low oxygen content gas being pre-chilled to 60-100 ℃, be cooled to 20-60 ℃, be cooled to 0-20 ℃ by condenser again, collect the organic solvent that condensation obtains, be reused for desorption after the low oxygen content gas of condenser output is preheating to 0-40 ℃; When being lower than, the temperature of absorber finishes desorption when 140 ℃ and desorption time reach 3-6h.
Further, described low oxygen content gas by with air and nitrogen, carbon dioxide or the combustion product gases after purifying mix and obtain, its oxygen content is lower than 10vol%.
Adsorbent in the described absorber is an active carbon.
The present invention also provides the device that adopts said method reclaiming clean organic solvent, it is characterized in that, comprise first heat exchanger, first heat exchanger connects first air cooler, first air cooler is connected first absorber and second absorber by first valve respectively with the 5th valve, first absorber is connected first blower fan by second valve with the 7th valve respectively with second absorber, and first blower fan connects first heat exchanger;
First absorber is connected second blower fan by the 4th valve with the 8th valve respectively with second absorber, second blower fan connects gas bomb by the 14 valve, second blower fan connects oil heater, the heating oil-in of oil heater is connected oil oven respectively with outlet, and oil heater is connected first absorber and second absorber by the 3rd valve respectively with the 6th valve;
Pipeline between second blower fan and the oil heater exports by the 11 valve is connected second heat exchanger with the 12 valve hot gas inlet and cold air respectively, the hot gas outlet of second heat exchanger connects second air cooler, second air cooler is connected the 3rd blower fan via first condenser with second condenser successively, the 3rd blower fan connects the cold air inlet of second heat exchanger, the refrigerant exit of first condenser and second condenser is connected water cooler, second heat exchanger respectively with inlet, the bottom solvent outlet of first condenser and second condenser is connected the solvent recovery case respectively.
Further, pipeline between first valve and first absorber is connected with the branch road of the 9th valve, pipeline between the 5th valve and second absorber is connected with the branch road of the tenth valve, the branch road that is provided with the 9th valve is connected oxygen sensor respectively with the branch road that is provided with the tenth valve, and oxygen sensor connects the export pipeline of first air cooler.
Connect by the pipeline that is provided with the 19 valve between the hot gas export pipeline of the export pipeline of first air cooler and second heat exchanger.
Be provided with cooling water pipeline in first absorber and second absorber, the inlet of the cooling water pipeline of first absorber and second absorber is respectively equipped with the 16 valve and the 17 valve, outlet are respectively equipped with the 23 valve and the 24 valve.
The throughput of described second blower fan is the 20-150% of first blower fan.
Outlet is connected first spark arrester and second spark arrester respectively with cold air in the hot gas import of described first heat exchanger.
The volume of pipeline is 2-20 times that adsorbent loads volume in first absorber or second absorber between described first spark arrester to the first absorber or second absorber.
The present invention is according to the type of solvent, and the rate of recovery situation of requirement is selected type, adsorption temp, the humidity of control adsorbate, the type of regeneration media and the material of equipment of absorption with active carbon.The material of equipment comprises the alloy of carbon steel, stainless steel or some type.Determine the form of absorber container according to the flow of gas.The refrigerant of regenerative process and heating agent fibrous root are determined according to user's actual conditions.
Desorption process adopts band shunting gas circuit mode among the present invention.Gas is heated to and enters absorber after the uniform temperature it is carried out desorption.After gas is heated to the regular hour, part adds and is rich in organic gas behind the thermal desorption and enters cools down by the by-pass shunt system, obtaining the partial organic substances cooling fluid reclaims, remainder gas enters the further condensation of condenser, the organic matter condensate liquid that obtains after the condensation reclaims, uncooled portion gas in the condensation enters heat exchanger heats, comes back to the air-flow heating systems.After arriving the setting desorption time, control system makes absorber withdraw from detachment status by the process control valve, after air-cooled, prepares the adsorption process that enters following one-period.
The present invention can further reduce the energy consumption of gas heating and cooling in the shunting condenser system by treating to set second heat exchanger between condensed gas and condensation final vacuum, thereby reduces the cost that organic matter reclaims.
The present invention compares with the steam desorb, and the condensed water secondary pollution of hot gas desorb seldom.The organic matter water content low (for the more apparent advantage of water miscible organic matter) that reclaims is convenient to further refining the recovery or direct same usefulness, and the time of regeneration of adsorbent beds drying, cooling is shorter, and is relatively low to the adsorption system material requirements.The desorb of carrying out adsorbent by low oxygen-containing gas closed-circuit system has following benefit: (1) closed circuit dividing potential drop that improves organic gas under the situation that does not influence rate of heat transfer effectively, help condensation separation, (2) because closed circuit, controlled the total oxygen in the loop gas, make that the possibility of organic matter generation chemical change reduces greatly in the regenerative process, it is better to reclaim organic quality, and (3) low to be contained the oxygen total amount and guaranteed security of system.The present invention has improved the efficiency of energy utilization of desorption process effectively under the prerequisite that guarantees the recovery yield, the recovery organic matter purity height that obtains simultaneously, and follow-up refining expense is low, has expanded adsorbing separation, has adsorbed the range of application that reclaims gaseous contaminant.
The present invention can be used for the gaseous contamination purification and organic solvent reclaims occasion, is particularly suitable for water-soluble, facile hydrolysis organic solvent tail gas recycle, and it reclaims yield greater than 90%.The recyclable purification boiling point of the present invention is at most solvents of 20 ℃～200 ℃ of scopes, as benzene,toluene,xylene, ethylbenzene, cyclohexane, acetone, ethanol, isopropyl alcohol, ethyl acetate, dimethyl formamide, dimethylacetylamide, gasoline, CS
2, CCl
4, HCCl
3, RCCl
2Deng.
Description of drawings
Fig. 1 is a kind of organic solvent reclaiming clean device schematic diagram.
The specific embodiment
Specify the present invention below in conjunction with embodiment.
Embodiment 1
A kind of organic solvent reclaiming clean device is by first heat exchanger 1, first air cooler 2, first absorber 3, second absorber 4, first blower fan 5, oil oven 6, second blower fan 7, oil heater 8, second heat exchanger 9, second air cooler 10, first condenser 11, second condenser 12, the 3rd blower fan 13, water cooler 14, gas bomb 15, solvent recovery case 16, first spark arrester 17, second spark arrester 18, first valve 19, the 5th valve 20, second valve 21, the 7th valve 22, the 4th valve 23, the 8th valve 24, the 14 valve 25, the 6th valve 26, the 3rd valve 27, the 11 valve 28, the 12 valve 29, the 9th valve 30, the tenth valve 31, the 13 valve 32, the 15 valve 33, the 16 valve 34, the 17 valve 35, oxygen sensor 36, the 19 valve 37, the 20 valve 38, the 21 valve 39, the 23 valve 40, the 24 valve 41, temperature transmitter 42, pressure transmitter 43, thermometer 44, first ball valve 45, second ball valve 46 and look handleless cup 47 and form.
First heat exchanger 1 connects first air cooler 2, first air cooler 2 is connected first absorber 3 and second absorber 4 by first valve 19 respectively with the 5th valve 20, first absorber 3 is connected first blower fan, 5, the first blower fans 5 by second valve 21 respectively with second absorber 4 and connects first heat exchanger 1 with the 7th valve 22;
First absorber 3 is connected second blower fan 7 by the 4th valve 23 with the 8th valve 24 respectively with second absorber 4, second blower fan 7 connects gas bomb 15 by the 14 valve 25, second blower fan 7 connects oil heater 8, the heating oil-in of oil heater 8 is connected oil oven 6 respectively with outlet, and oil heater 8 is connected first absorber 3 and second absorber 4 by the 3rd valve 27 respectively with the 6th valve 26;
Pipeline between second blower fan 7 and the oil heater 8 exports by the 11 valve 28 is connected second heat exchanger 9 with the 12 valve 29 hot gas inlet and cold air respectively, the hot gas outlet of second heat exchanger 9 connects second air cooler 10, second air cooler 10 is connected the 3rd blower fan 13 via first condenser 11 with second condenser 12 successively, the 3rd blower fan 13 connects the cold air inlet of second heat exchanger 9, the refrigerant exit of first condenser 11 and second condenser 12 is connected water cooler 14, the second heat exchangers 9 respectively with inlet, first condenser 11 is connected solvent recovery case 16 respectively with the bottom solvent outlet of second condenser 12.
Pipeline between first valve 19 and first absorber 3 is connected with the branch road of the 9th valve 30, pipeline between the 5th valve 20 and second absorber 4 is connected with the branch road of the tenth valve 31, the branch road that is provided with the 9th valve 30 is connected oxygen sensor 36 respectively with the branch road that is provided with the tenth valve 31, and oxygen sensor 36 connects the export pipeline of first air cooler 2.Open the 9th valve 30/ the tenth valve 31 when opening first valve 19/ the 5th valve 20, the oxygen concentration that senses when oxygen sensor 36 surpasses 10vol%, open the 14 valve 25,, close the 14 valve 25, close the 9th valve 30 and the tenth valve 31 simultaneously up to recovering oxygen concentration.
Connect by the pipeline that is provided with the 19 valve 37 between the hot gas export pipeline of the export pipeline of first air cooler 2 and second heat exchanger 9, be used for equilibrium oxygen concentration.When opening the 11 valve 28 and the 12 valve 29, open the 19 valve 37, close the 19 valve 37 when closing the 9th valve 30 and the tenth valve 31.
Be provided with cooling water pipeline in first absorber 3 and second absorber 4, the inlet of the cooling water pipeline of first absorber 3 and second absorber 4 is respectively equipped with the 16 valve 34 and the 17 valve 35, outlet are respectively equipped with the 23 valve 40 and the 24 valve 41.Cooling water enters first absorber 3 and second absorber 4 via the 16 valve 34 and the 17 valve 35, discharges via the 23 valve 40 and the 24 valve 41 afterwards.The 15 valve 33 is an air bleeding valve.Do not have under the normal situation of opening at the 16 valve 34 and the 17 valve 35, first ball valve 45 and second ball valve 46 are opened automatically.When the temperature of first absorber 3 and second absorber 4 surpasses 200 ℃, open the 16 valve the 34, the 17 valve the 35, the 23 valve 40 and the 24 valve 41, other all valve closings.
Outlet is connected first spark arrester 17 and second spark arrester 18 respectively with cold air in the hot gas import of described first heat exchanger 1.The throughput of described second blower fan 7 is 20-150% of first blower fan 5.The volume of pipeline is 2-20 times that adsorbent loads volume in first absorber 3 or second absorber 4 between described first spark arrester, 17 to first absorbers 3 or second absorber 4.Look handleless cup 47 and be located between solvent recovery case 16 and the 13 valve the 32, the 20 valve the 38, the 21 valve 39, be used for observing the flow that reclaims solvent.
This device can be automatic control, and the PLC input connects oxygen sensor 36, temperature transmitter 42 and pressure transmitter 43, and output connects all valves.
It is 1: 25 water and ethylene glycol mixture that refrigerant in described first condenser 11 and second condenser 12 is respectively volume ratio.The deep fat that adds in the described oil heater 8 is conduction oil Q/TCOW.
With first absorber 3 is example, and the method for said apparatus reclaiming clean organic solvent is as follows:
To contain organic solvents such as dimethylbenzene, petroleum hydrocarbon and be pre-chilled to 40 ℃, be cooled to 10 ℃ again, open first valve 19 and second valve 21, waste gas cooled will be fed first absorber 3, will be through output behind the heating by the exhaust gases to 100 of adsorption treatment ℃; When organic solvent strength was 2000ppm, adsorption time was generally 8 hours.After adsorption time arrives, close first valve 19 and second valve 21, open the 3rd valve 27 and the 4th valve 23, open oil heater 8 and oil oven 6, open second blower fan 7 after 10 minutes, the low oxygen content gas that is preheating to 150 ℃ is fed first absorber 3 carry out desorption; When the temperature of absorber surpasses 90 ℃ and desorption time and reaches 15min, open the 11 valve 28 and the 12 valve 29, after constantly 1/100 low oxygen content gas being pre-chilled to 60 ℃, be cooled to 20 ℃, again by condensing to 0 ℃, collect the organic solvent that condensation obtains, be reused for desorption after the low oxygen content gas of condenser output is preheating to 0 ℃; When the temperature of absorber is lower than 140 ℃ and desorption time and reaches 3h, close the 11 valve the 28, the 12 valve 29, the 3rd valve 27 and the 4th valve 23 and finish desorption.
With second absorber 4 is example, and the method for said apparatus reclaiming clean organic solvent is as follows:
To contain organic solvents such as dimethylbenzene, petroleum hydrocarbon and be pre-chilled to 40 ℃, be cooled to 10 ℃ again, open the 5th valve 20 and the 7th valve 22, waste gas cooled will be fed first absorber 3, will be through output behind the heating by the exhaust gases to 100 of adsorption treatment ℃; When organic solvent strength was 2000ppm, adsorption time was generally 8 hours.After adsorption time arrives, close the 5th valve 20 and the 7th valve 22, open the 8th valve 24 and the 6th valve 26, open oil heater 8 and oil oven 6, open second blower fan 7 after 10 minutes, the low oxygen content gas that is preheating to 150 ℃ is fed first absorber 3 carry out desorption; When the temperature of absorber surpasses 90 ℃ and desorption time and reaches 15min, open the 11 valve 28 and the 12 valve 29, after constantly 1/100 low oxygen content gas being pre-chilled to 60 ℃, be cooled to 20 ℃, again by condensing to 0 ℃, collect the organic solvent that condensation obtains, be reused for desorption after the low oxygen content gas of condenser output is preheating to 0 ℃; When the temperature of absorber is lower than 140 ℃ and desorption time and reaches 3h, close the 11 valve the 28, the 12 valve 29, the 8th valve 24 and the 6th valve 26 and finish desorption.
First absorber 3 and the second absorber 4 desorption program that hockets guarantees that at least one absorber is in adsorbed state.
Described low oxygen content gas obtains by air is mixed with nitrogen, and its oxygen content is lower than 10vol%.Adsorbent in the described absorber is an active carbon.
Embodiment 2
Adopting embodiment 1 described device, is example with first absorber 3, and the method for said apparatus reclaiming clean organic solvent is as follows:
To contain organic solvents such as dimethylbenzene, petroleum hydrocarbon and be pre-chilled to 100 ℃, be cooled to 40 ℃ again, open first valve 19 and second valve 21, waste gas cooled will be fed first absorber 3, will be through output behind the heating by the exhaust gases to 200 of adsorption treatment ℃; When organic solvent strength was 2000ppm, adsorption time was generally 8 hours.After adsorption time arrives, close first valve 19 and second valve 21, open the 3rd valve 27 and the 4th valve 23, open oil heater 8 and oil oven 6, open second blower fan 7 after 10 minutes, the low oxygen content gas that is preheating to 300 ℃ is fed first absorber 3 carry out desorption; When the temperature of absorber surpasses 90 ℃ and desorption time and reaches 30min, open the 11 valve 28 and the 12 valve 29, after constantly 1/2 low oxygen content gas being pre-chilled to 100 ℃, be cooled to 60 ℃, again by condensing to 20 ℃, collect the organic solvent that condensation obtains, be reused for desorption after the low oxygen content gas of condenser output is preheating to 40 ℃; When the temperature of absorber is lower than 140 ℃ and desorption time and reaches 6h, close the 11 valve the 28, the 12 valve 29, the 3rd valve 27 and the 4th valve 23 and finish desorption.
With second absorber 4 is example, and the method for said apparatus reclaiming clean organic solvent is as follows:
To contain organic solvents such as dimethylbenzene, petroleum hydrocarbon and be pre-chilled to 100 ℃, be cooled to 40 ℃ again, open the 5th valve 20 and the 7th valve 22, waste gas cooled will be fed first absorber 3, will be through output behind the heating by the exhaust gases to 200 of adsorption treatment ℃; When organic solvent strength was 2000ppm, adsorption time was generally 8 hours.After adsorption time arrives, close the 5th valve 20 and the 7th valve 22, open the 8th valve 24 and the 6th valve 26, open oil heater 8 and oil oven 6, open second blower fan 7 after 10 minutes, the low oxygen content gas that is preheating to 300 ℃ is fed first absorber 3 carry out desorption; When the temperature of absorber surpasses 90 ℃ and desorption time and reaches 30min, open the 11 valve 28 and the 12 valve 29, after constantly 1/2 low oxygen content gas being pre-chilled to 100 ℃, be cooled to 60 ℃, again by condensing to 20 ℃, collect the organic solvent that condensation obtains, be reused for desorption after the low oxygen content gas of condenser output is preheating to 0-40 ℃; When the temperature of absorber is lower than 140 ℃ and desorption time and reaches 6h, close the 11 valve the 28, the 12 valve 29, the 8th valve 24 and the 6th valve 26 and finish desorption.
First absorber 3 and the second absorber 4 desorption program that hockets guarantees that at least one absorber is in adsorbed state.
Described low oxygen content gas is by obtaining air and carbon dioxide mix, and its oxygen content is lower than 10vol%.Adsorbent in the described absorber is an active carbon.
Embodiment 3
Adopting embodiment 1 described device, is example with first absorber 3, and the method for said apparatus reclaiming clean organic solvent is as follows:
To contain organic solvents such as dimethylbenzene, petroleum hydrocarbon and be pre-chilled to 60 ℃, be cooled to 20 ℃ again, open first valve 19 and second valve 21, waste gas cooled will be fed first absorber 3, will be through output behind the heating by the exhaust gases to 150 of adsorption treatment ℃; When organic solvent strength was 2000ppm, adsorption time was generally 8 hours.After adsorption time arrives, close first valve 19 and second valve 21, open the 3rd valve 27 and the 4th valve 23, open oil heater 8 and oil oven 6, open second blower fan 7 after 10 minutes, the low oxygen content gas that is preheating to 200 ℃ is fed first absorber 3 carry out desorption; When the temperature of absorber surpasses 90 ℃ and desorption time and reaches 20min, open the 11 valve 28 and the 12 valve 29, after constantly 1/3 low oxygen content gas being pre-chilled to 80 ℃, be cooled to 40 ℃, again by condensing to 10 ℃, collect the organic solvent that condensation obtains, be reused for desorption after the low oxygen content gas of condenser output is preheating to 20 ℃; When the temperature of absorber is lower than 140 ℃ and desorption time and reaches 5h, close the 11 valve the 28, the 12 valve 29, the 3rd valve 27 and the 4th valve 23 and finish desorption.
With second absorber 4 is example, and the method for said apparatus reclaiming clean organic solvent is as follows:
To contain organic solvents such as dimethylbenzene, petroleum hydrocarbon and be pre-chilled to 60 ℃, be cooled to 20 ℃ again, open the 5th valve 20 and the 7th valve 22, waste gas cooled will be fed first absorber 3, will be through output behind the heating by the exhaust gases to 150 of adsorption treatment ℃; When organic solvent strength was 2000ppm, adsorption time was generally 8 hours.After adsorption time arrives, close the 5th valve 20 and the 7th valve 22, open the 8th valve 24 and the 6th valve 26, open oil heater 8 and oil oven 6, open second blower fan 7 after 10 minutes, the low oxygen content gas that is preheating to 200 ℃ is fed first absorber 3 carry out desorption; When the temperature of absorber surpasses 90 ℃ and desorption time and reaches 15-30min, open the 11 valve 28 and the 12 valve 29, after constantly 1/3 low oxygen content gas being pre-chilled to 80 ℃, be cooled to 40 ℃, again by condensing to 10 ℃, collect the organic solvent that condensation obtains, be reused for desorption after the low oxygen content gas of condenser output is preheating to 20 ℃; When the temperature of absorber is lower than 140 ℃ and desorption time and reaches 5h, close the 11 valve the 28, the 12 valve 29, the 8th valve 24 and the 6th valve 26 and finish desorption.
First absorber 3 and the second absorber 4 desorption program that hockets guarantees that at least one absorber is in adsorbed state.
Described low oxygen content gas by with air with purify after combustion product gases mix and obtain, its oxygen content is lower than 10vol%.Adsorbent in the described absorber is an active carbon.
Claims (9)
1. an organic solvent recovery and purification method is characterized in that, concrete steps are:
The waste gas that will contain organic solvent is pre-chilled to 40-100 ℃, is cooled to 10-40 ℃ again, and waste gas cooled is fed at least one absorber, will export after 100-200 ℃ through the heating by the exhaust gases of adsorption treatment;
Wherein, the desorption of described absorber is: the low oxygen content gas feeding absorber that will be preheating to 150-300 ℃ carries out desorption; When the temperature of absorber surpasses 90 ℃ and desorption time and reaches 15-30min, after constantly 1/100-1/2 low oxygen content gas being pre-chilled to 60-100 ℃, be cooled to 20-60 ℃, be cooled to 0-20 ℃ by condenser again, collect the organic solvent that condensation obtains, be reused for desorption after the low oxygen content gas of condenser output is preheating to 0-40 ℃; When being lower than, the temperature of absorber finishes desorption when 140 ℃ and desorption time reach 3-6h; Described low oxygen content gas by with air and nitrogen, carbon dioxide or the combustion product gases after purifying mix and obtain, its oxygen content is lower than 10vol%.
2. method according to claim 1 is characterized in that the adsorbent in the described absorber is an active carbon.
3. adopt the device of the described method reclaiming clean of claim 1 organic solvent, it is characterized in that, comprise first heat exchanger (1), first heat exchanger (1) connects first air cooler (2), first air cooler (2) is connected first absorber (3) and second absorber (4) by first valve (19) respectively with the 5th valve (20), first absorber (3) is connected first blower fan (5) by second valve (21) with the 7th valve (22) respectively with second absorber (4), and first blower fan (5) connects first heat exchanger (1);
First absorber (3) is connected second blower fan (7) by the 4th valve (23) with the 8th valve (24) respectively with second absorber (4), second blower fan (7) connects gas bomb (15) by the 14 valve (25), second blower fan (7) connects oil heater (8), the heating oil-in of oil heater (8) is connected oil oven (6) respectively with outlet, and oil heater (8) is connected first absorber (3) and second absorber (4) by the 3rd valve (27) respectively with the 6th valve (26);
Pipeline between second blower fan (7) and the oil heater (8) exports by the 11 valve (28) is connected second heat exchanger (9) with the 12 valve (29) hot gas inlet and cold air respectively, the hot gas outlet of second heat exchanger (9) connects second air cooler (10), second air cooler (10) is connected the 3rd blower fan (13) via first condenser (11) with second condenser (12) successively, the 3rd blower fan (13) connects the cold air inlet of second heat exchanger (9), the refrigerant exit of first condenser (11) and second condenser (12) is connected water cooler (14), second heat exchanger (9) respectively with inlet, the bottom solvent outlet of first condenser (11) and second condenser (12) is connected solvent recovery case (16) respectively.
4. device as claimed in claim 3, it is characterized in that, pipeline between first valve (19) and first absorber (3) is connected with the branch road of the 9th valve (30), pipeline between the 5th valve (20) and second absorber (4) is connected with the branch road of the tenth valve (31), the branch road that is provided with the 9th valve (30) is connected oxygen sensor (36) respectively with the branch road that is provided with the tenth valve (31), and oxygen sensor (36) connects the export pipeline of first air cooler (2).
5. device as claimed in claim 3 is characterized in that, connects by the pipeline that is provided with the 19 valve (37) between the hot gas export pipeline of the export pipeline of first air cooler (2) and second heat exchanger (9).
6. device as claimed in claim 3, it is characterized in that, be provided with cooling water pipeline in first absorber (3) and second absorber (4), the inlet of the cooling water pipeline of first absorber (3) and second absorber (4) is respectively equipped with the 16 valve (34) and the 17 valve (35), outlet are respectively equipped with the 23 valve (40) and the 24 valve (41).
7. device as claimed in claim 3 is characterized in that, the throughput of described second blower fan (7) is the 20-150% of first blower fan (5).
8. device as claimed in claim 3 is characterized in that, outlet is connected first spark arrester (17) and second spark arrester (18) respectively with cold air in the hot gas import of described first heat exchanger (1).
9. device as claimed in claim 8 is characterized in that, described first spark arrester (17) to the volume of pipeline between first absorber (3) or second absorber (4) is 2-20 times that adsorbent loads volume in first absorber (3) or second absorber (4).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100476411A CN101530713B (en) | 2009-03-16 | 2009-03-16 | Recovering and purifying device of organic solvent and method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100476411A CN101530713B (en) | 2009-03-16 | 2009-03-16 | Recovering and purifying device of organic solvent and method |
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| Publication Number | Publication Date |
|---|---|
| CN101530713A CN101530713A (en) | 2009-09-16 |
| CN101530713B true CN101530713B (en) | 2011-07-27 |
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| CN2009100476411A Active CN101530713B (en) | 2009-03-16 | 2009-03-16 | Recovering and purifying device of organic solvent and method |
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| CN107469568A (en) * | 2017-09-07 | 2017-12-15 | 无锡普爱德环保科技有限公司 | VOC runner performance method of testings |
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| CN102218253A (en) * | 2010-04-19 | 2011-10-19 | 杰智环境科技股份有限公司 | Device and method for reducing oxidation degree of adsorbed solvent |
| CN104436742B (en) * | 2014-10-20 | 2016-05-25 | 宜宾丝丽雅股份有限公司 | CS produced by viscose staple fiber2Recovery process |
| WO2023070415A1 (en) * | 2021-10-28 | 2023-05-04 | 南京沿江资源生态科学研究院有限公司 | Organic solvent harmless treatment system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107469568A (en) * | 2017-09-07 | 2017-12-15 | 无锡普爱德环保科技有限公司 | VOC runner performance method of testings |
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Address after: 200092, room 235, 827 Changyang Road, Shanghai, Yangpu District Patentee after: Shanghai Tongji construction Polytron Technologies Inc Address before: 200092, room 235, 827 Changyang Road, Shanghai, Yangpu District Patentee before: Tongji Constructing Science & Technology Co., Ltd., Shanghai |